US20120104322A1 - Processes and systems for producing syngas from methane - Google Patents
Processes and systems for producing syngas from methane Download PDFInfo
- Publication number
- US20120104322A1 US20120104322A1 US12/917,781 US91778110A US2012104322A1 US 20120104322 A1 US20120104322 A1 US 20120104322A1 US 91778110 A US91778110 A US 91778110A US 2012104322 A1 US2012104322 A1 US 2012104322A1
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- component
- catalyst system
- methane
- perovskite
- apatite
- Prior art date
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Links
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 136
- 238000000034 method Methods 0.000 title claims abstract description 43
- 239000003054 catalyst Substances 0.000 claims abstract description 95
- 239000007789 gas Substances 0.000 claims abstract description 46
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 44
- 238000006243 chemical reaction Methods 0.000 claims abstract description 33
- 229910052586 apatite Inorganic materials 0.000 claims abstract description 31
- VSIIXMUUUJUKCM-UHFFFAOYSA-D pentacalcium;fluoride;triphosphate Chemical compound [F-].[Ca+2].[Ca+2].[Ca+2].[Ca+2].[Ca+2].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O VSIIXMUUUJUKCM-UHFFFAOYSA-D 0.000 claims abstract description 31
- 229910002091 carbon monoxide Inorganic materials 0.000 claims abstract description 26
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 13
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 13
- 239000001257 hydrogen Substances 0.000 claims abstract description 13
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 24
- 239000001301 oxygen Substances 0.000 claims description 24
- 229910052760 oxygen Inorganic materials 0.000 claims description 24
- 239000000203 mixture Substances 0.000 claims description 22
- 239000002245 particle Substances 0.000 claims description 9
- 229910052759 nickel Inorganic materials 0.000 claims description 7
- 230000008929 regeneration Effects 0.000 claims description 7
- 238000011069 regeneration method Methods 0.000 claims description 7
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- 238000004891 communication Methods 0.000 claims description 6
- 239000012530 fluid Substances 0.000 claims description 6
- 229910052588 hydroxylapatite Inorganic materials 0.000 claims description 6
- XYJRXVWERLGGKC-UHFFFAOYSA-D pentacalcium;hydroxide;triphosphate Chemical compound [OH-].[Ca+2].[Ca+2].[Ca+2].[Ca+2].[Ca+2].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O XYJRXVWERLGGKC-UHFFFAOYSA-D 0.000 claims description 6
- 229910052746 lanthanum Inorganic materials 0.000 claims description 5
- 229910052712 strontium Inorganic materials 0.000 claims description 5
- 229910052723 transition metal Inorganic materials 0.000 claims description 5
- 150000003624 transition metals Chemical class 0.000 claims description 5
- 229910052693 Europium Inorganic materials 0.000 claims description 4
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- 229910052779 Neodymium Inorganic materials 0.000 claims description 4
- 229910052777 Praseodymium Inorganic materials 0.000 claims description 4
- 229910052772 Samarium Inorganic materials 0.000 claims description 4
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 4
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- 150000003818 basic metals Chemical group 0.000 claims description 3
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- 229910052684 Cerium Inorganic materials 0.000 claims description 2
- 229910052692 Dysprosium Inorganic materials 0.000 claims description 2
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- 229910052689 Holmium Inorganic materials 0.000 claims description 2
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- 229910052701 rubidium Inorganic materials 0.000 claims description 2
- 229910052708 sodium Inorganic materials 0.000 claims description 2
- 229910052719 titanium Inorganic materials 0.000 claims description 2
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- 229910052745 lead Inorganic materials 0.000 claims 1
- 229910052706 scandium Inorganic materials 0.000 claims 1
- 229910052725 zinc Inorganic materials 0.000 claims 1
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 17
- 230000003647 oxidation Effects 0.000 description 17
- 238000007254 oxidation reaction Methods 0.000 description 17
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 14
- 239000003546 flue gas Substances 0.000 description 10
- 229910002092 carbon dioxide Inorganic materials 0.000 description 9
- 239000001569 carbon dioxide Substances 0.000 description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 8
- 239000000571 coke Substances 0.000 description 7
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 7
- 239000000047 product Substances 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 5
- 229910052751 metal Inorganic materials 0.000 description 5
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- 230000000694 effects Effects 0.000 description 4
- 239000011734 sodium Substances 0.000 description 4
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 3
- 239000007795 chemical reaction product Substances 0.000 description 3
- 239000010949 copper Substances 0.000 description 3
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- 239000011572 manganese Substances 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 230000001172 regenerating effect Effects 0.000 description 3
- 238000012216 screening Methods 0.000 description 3
- 238000000629 steam reforming Methods 0.000 description 3
- 238000003786 synthesis reaction Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 2
- 229910019902 La0.8Sr0.2FeO3 Inorganic materials 0.000 description 2
- 125000002091 cationic group Chemical group 0.000 description 2
- 239000000460 chlorine Substances 0.000 description 2
- 239000011651 chromium Substances 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 2
- 239000011777 magnesium Substances 0.000 description 2
- 229910044991 metal oxide Inorganic materials 0.000 description 2
- 150000004706 metal oxides Chemical class 0.000 description 2
- 150000002739 metals Chemical class 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 238000001991 steam methane reforming Methods 0.000 description 2
- 239000010936 titanium Substances 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical group [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- PXGOKWXKJXAPGV-UHFFFAOYSA-N Fluorine Chemical compound FF PXGOKWXKJXAPGV-UHFFFAOYSA-N 0.000 description 1
- GYHNNYVSQQEPJS-UHFFFAOYSA-N Gallium Chemical compound [Ga] GYHNNYVSQQEPJS-UHFFFAOYSA-N 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 1
- 229910052773 Promethium Inorganic materials 0.000 description 1
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 1
- 229910052768 actinide Inorganic materials 0.000 description 1
- 150000001255 actinides Chemical class 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 125000004429 atom Chemical group 0.000 description 1
- DSAJWYNOEDNPEQ-UHFFFAOYSA-N barium atom Chemical compound [Ba] DSAJWYNOEDNPEQ-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- BDOSMKKIYDKNTQ-UHFFFAOYSA-N cadmium atom Chemical compound [Cd] BDOSMKKIYDKNTQ-UHFFFAOYSA-N 0.000 description 1
- TVFDJXOCXUVLDH-UHFFFAOYSA-N caesium atom Chemical compound [Cs] TVFDJXOCXUVLDH-UHFFFAOYSA-N 0.000 description 1
- 238000001193 catalytic steam reforming Methods 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 229910017052 cobalt Inorganic materials 0.000 description 1
- 239000010941 cobalt Substances 0.000 description 1
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- UYAHIZSMUZPPFV-UHFFFAOYSA-N erbium Chemical compound [Er] UYAHIZSMUZPPFV-UHFFFAOYSA-N 0.000 description 1
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- 239000011737 fluorine Substances 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- UIWYJDYFSGRHKR-UHFFFAOYSA-N gadolinium atom Chemical compound [Gd] UIWYJDYFSGRHKR-UHFFFAOYSA-N 0.000 description 1
- KJZYNXUDTRRSPN-UHFFFAOYSA-N holmium atom Chemical compound [Ho] KJZYNXUDTRRSPN-UHFFFAOYSA-N 0.000 description 1
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- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 1
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- OHSVLFRHMCKCQY-UHFFFAOYSA-N lutetium atom Chemical compound [Lu] OHSVLFRHMCKCQY-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
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- QEFYFXOXNSNQGX-UHFFFAOYSA-N neodymium atom Chemical compound [Nd] QEFYFXOXNSNQGX-UHFFFAOYSA-N 0.000 description 1
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- 239000011591 potassium Substances 0.000 description 1
- PUDIUYLPXJFUGB-UHFFFAOYSA-N praseodymium atom Chemical compound [Pr] PUDIUYLPXJFUGB-UHFFFAOYSA-N 0.000 description 1
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- 230000001360 synchronised effect Effects 0.000 description 1
- JBQYATWDVHIOAR-UHFFFAOYSA-N tellanylidenegermanium Chemical compound [Te]=[Ge] JBQYATWDVHIOAR-UHFFFAOYSA-N 0.000 description 1
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Images
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/002—Mixed oxides other than spinels, e.g. perovskite
-
- B01J35/19—
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J38/00—Regeneration or reactivation of catalysts, in general
- B01J38/04—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst
- B01J38/12—Treating with free oxygen-containing gas
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J38/00—Regeneration or reactivation of catalysts, in general
- B01J38/04—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst
- B01J38/12—Treating with free oxygen-containing gas
- B01J38/22—Moving bed, e.g. vertically or horizontally moving bulk
- B01J38/28—Moving bed, e.g. vertically or horizontally moving bulk having mainly concurrent flow of oxygen-containing gas and material
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
- C01B3/42—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts using moving solid particles
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2523/00—Constitutive chemical elements of heterogeneous catalysts
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/025—Processes for making hydrogen or synthesis gas containing a partial oxidation step
- C01B2203/0261—Processes for making hydrogen or synthesis gas containing a partial oxidation step containing a catalytic partial oxidation step [CPO]
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/10—Catalysts for performing the hydrogen forming reactions
- C01B2203/1041—Composition of the catalyst
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
Definitions
- the present invention relates generally to processes and systems for producing synthesis gas, and more particularly relates to processes and systems for producing synthesis gas comprising hydrogen and carbon monoxide from a gas stream comprising methane.
- the formed gases are not useful for the production of valuable chemical compounds, and the stability of these products complicates their conversion to more desirable products. Also, further processing is problematic due to the high temperatures generated in the combustion reaction, presenting problems with respect to downstream reactors and catalysts.
- syngas useful gases, known as synthesis gas or “syngas”, are produced in the conversion of methane to a gas mixture containing hydrogen and carbon monoxide, for example, according to one of the following reactions:
- the last reaction is the most desirable in terms of both quality of the syngas produced and the minimization of the heat liberated to protect the apparatus and catalyst bed from thermal damage.
- syngas-generating processes include steam methane reforming and methane partial oxidation (also referred to as catalytic partial oxidation).
- steam methane reforming and methane partial oxidation also referred to as catalytic partial oxidation
- the choice of a particular route depends primarily on the desired product composition, as determined by its end use.
- the syngas is typically used to produce methanol, ammonia, or heavier hydrocarbon fuels through Fisher-Tropsch technology for example.
- the methane-containing and oxygen-containing feeds are mixed and reacted in a diffusion flame.
- the oxidized effluent is then passed into a steam reforming reactor zone where the effluent is contacted with a conventional steam reforming catalyst.
- the catalyst may be present as a simple fixed bed or impregnated into a monolith carrier or ceramic foam.
- the high temperatures and pressures in the catalytic steam reforming reactor zone place great demands on the reactor, in terms of thermal resistance to damage and operational cost, and on the reforming catalyst, in terms of the catalyst's ability to substantially retain its catalytic activity and stability over many years of use due to substantial coking of the catalyst.
- some of the methane may be burned to provide heat for the energy intensive process and therefore, complete conversion of the methane to the desired end product is not achieved thereby reducing the overall selectivity of the process.
- methane is passed along a nickel-based catalyst for example, and burned at a high temperature in an oxygen lean environment where the methane is partially oxidized to carbon monoxide along with the production of hydrogen and some steam.
- the methane partial oxidation process uses a higher concentration of oxygen than is found in air and, therefore, requires the use of a costly air separation unit to supply the higher concentration of oxygen.
- the methane partial oxidation process typically burns a portion of the methane to provide heat for the energy intensive process and therefore, complete conversion of the methane to the desired end product is not achieved thereby reducing the overall selectivity of the process.
- the methane partial oxidation process results in a substantial amount of coke being deposited onto the catalyst and therefore, catalyst activity and stability over time is substantially reduced.
- a process for producing syngas comprising hydrogen and carbon monoxide from a gas stream comprising methane comprises the step of contacting the gas stream with a two-component catalyst system comprising an apatite component and a perovskite component at reaction conditions effective to convert the methane to the syngas.
- a system for producing syngas comprising hydrogen and carbon monoxide from a feed gas stream comprising methane comprises a reactor containing a two-component catalyst system comprising an apatite component and a perovskite component.
- the reactor is configured to receive the feed gas stream and to operate at reactor conditions effective to convert the methane to the syngas thereby converting the two-component catalyst system to a spent two-component catalyst system.
- FIG. 1 schematically illustrates a system for producing syngas from a feed gas stream comprising methane in accordance with an exemplary embodiment
- FIG. 2 is a flowchart of a process for producing syngas from a gas stream comprising methane in accordance with an exemplary embodiment
- FIG. 3 schematically illustrates a system in a first configuration for producing syngas from a feed gas stream comprising methane in accordance with another exemplary embodiment
- FIG. 4 schematically illustrates the system depicted in FIG. 3 in a second configuration
- FIG. 5 is a graphical representation of carbon monoxide selectivity and methane conversion for various catalyst systems in accordance with an exemplary embodiment of the present invention.
- the various embodiments contemplated herein relate to processes and systems for producing syngas comprising hydrogen and carbon monoxide from a methane containing gas stream.
- the gas stream is contacted with a two-component catalyst system comprising an apatite component and a perovskite component at reaction conditions that convert the methane to syngas.
- the oxygen for the reaction is supplied by the perovskite component, which is a metal oxide, rather than by an oxygen containing gas stream that is supplied by an air separator or other costly source.
- the inventors have discovered that by using the two-component catalyst system with the apatite component, which in at least one embodiment is a nickel containing oxide, the hydrogen atoms become disassociated from the methane such that the methane is activated and readily reacts with the oxygen supplied from the perovskite component at rates that favor a relatively high carbon monoxide selectivity over the production of carbon dioxide or water.
- the syngas produced is of preferably high quality having a relatively high carbon monoxide and hydrogen content with reduced amounts of carbon dioxide and water.
- the inventors have found that by using the apatite component, which is unlike many other nickel catalyst used for the partial oxidation of methane, very little coke is deposited onto the two-component catalyst system.
- the two-component catalyst system when spent, it can be readily regenerated as needed to maintain catalyst activity and stability over time. Furthermore, regenerating the two-component catalyst produces heat that may be supplied to the reactor to at least partially satisfy the energy requirements, such as, for example, in a fluidized catalytic cracking arrangement (FCC), which thereby places less demand on the system compared to conventional processes in terms of thermal resistance to damage and operational cost.
- FCC fluidized catalytic cracking arrangement
- FIG. 1 a schematic depiction of an exemplary reactor and a regenerator system 10 in accordance with an exemplary embodiment of the present invention is provided.
- the system 10 is configured as a fluidized catalytic cracking (FCC) arrangement.
- the system 10 comprises a reactor 12 that is configured to receive a feed gas stream 30 comprising methane.
- the reactor 12 contains a two-component catalyst system comprising an apatite component and a perovskite component.
- the apatite component has a chemical composition on an anhydrous basis expressed by an empirical formula of:
- A is an alkali metal selected from the group consisting of lithium (Li), sodium (Na), potassium (K), rubidium (Rb), cesium (Cs), and mixtures thereof
- v is a mole ratio of A:D (i.e., a ratio of the moles of A to the moles of D) and varies from 0 to about 2
- B is a basic metal
- w is a mole ratio of B:D and varies from about 1 to about 3
- t is the weighted average valence of B and varies from about 2 to about 3
- E is a transition metal selected from the group consisting of nickel (Ni), vanadium (V), manganese (Mn), iron (Fe), cobalt (Co), copper (Cu), and mixtures thereof
- x is a mole ratio of E:D and varies from 0 to about 0.5
- D is a framework component selected from the group consisting of phosphorus (P), V, and mixtures thereof
- G is an ani
- G is the anionic species of OH, and the apatite is a hydroxyapatite structured component.
- E is Ni and the apatite component is a nickel-based hydroxyapatite structured component.
- the basic metal B is typically a metal with a rather large cationic radius, generally from about 0.85 ⁇ to about 1.40 ⁇ , and a cationic charge of +2 or +3.
- These metals are broadly found in the alkaline earth series, rare earth series, and in selected cases in both the transition metal series, such as Cd and Hg, and the main group metals such as lead (Pb).
- B is selected from the group consisting of Ca, strontium (Sr), cadmium (Cd), Pb, barium (Ba), lanthanum (La), europium (Eu), gadolinium (Gd), praseodymium (Pr), neodymium (Nd), samarium (Sm), yttrium (Y), ytterbium (Yb), and mixtures thereof.
- the perovskite component comprises perovskite having a chemical composition expressed by an empirical formula of:
- Ma and Ma' that are identical or different, are chosen from the families of the alkaline earths, the lanthanides or the actinides, more particularly from La, Ce, Pr, Nd, promethium (Pm), Sm, Eu, Gd, terbium (Tb), dysprosium (Dy), holmium (Ho), erbium (Er), thulium (Tm), Yb, lutetium (Lu), Y, magnesium (Mg), Ca, Sr, Ba, and mixtures thereof, Mb and Mb′, that are identical or different, represent one or more atoms chosen from transition metals, and more particularly from Sc, titanium (Ti), V, chromium (Cr), Mn, Fe, Co, Ni, Cu, zinc (Zn), gallium (Ga), and mixtures thereof, x and y, that are identical or different, are greater than or equal to 0 and less than or equal to about 1, and w is such that the perovskite has an electrically neutral structure.
- the two-component catalyst system is configured as particles where each particle comprises the apatite component and the perovskite component.
- the apatite component is crystallized onto the perovskite component to form the particles.
- both the apatite and perovskite components may be bound to a carrier, such as, for example, alumina or silica.
- the two-component catalyst system is a physical mixture of the apatite and perovskite components.
- the two-component catalyst system has a mole ratio of the apatite component to the perovskite component of from about 1:2 to about 2:1, and most preferably of about 1:1.
- a process for producing the syngas includes contacting the feed gas stream 30 with the two-component catalyst system (step 100 ) in the reactor 12 which is operating at reaction conditions effective to convert the methane to an effluent stream comprising syngas 13 which may be passed along for subsequent processing via line 15 .
- the reactor 12 is operating at a reaction temperature of about 650° C. or greater, and preferably at a reaction temperature of from about 850 to about 1000° C.
- the reactor 12 is operating at a reaction pressure of from about 15 to about 1000 psia, and preferably of from about 15 to about 600 psia, and more preferably of from about 15 to about 350 psia.
- the atmosphere inside the reactor 12 is substantially devoid of gaseous oxygen so that the oxygen source for the partial oxidation of methane comes primarily from the perovskite component.
- the inventors believe that by limiting the source of oxygen to the perovskite component, the partial oxidation of methane will primarily favor producing carbon monoxide and hydrogen over the more highly oxidized and undesirable products of carbon dioxide and water.
- the apatite component of the two-component catalyst system activates the methane (step 102 ) to form activated methane.
- the activated methane then readily oxidizes with oxygen from the perovskite component (step 104 ) to form the syngas 13 .
- the perovskite component becomes oxygen depleted, and a relatively small amount of carbonaceous byproduct, termed coke, is deposited on the two-component catalyst system reducing its catalytic activity and forming a spent two-component catalyst system.
- a regenerator 14 is in fluid communication with the reactor 12 to receive the spent two-component catalyst system via line 23 .
- the regenerator 14 is configured to receive an oxygen containing gas stream 22 , preferably air, from an outside source.
- the regenerator 14 operating at regeneration conditions receives the oxygen containing gas stream 22 , oxidizes the perovskite component and burns the coke off the spent two-component catalyst system to regenerate the spent two-component catalyst system (step 106 ) thereby producing a flue gas 26 that exits a flue gas line 28 to a flue gas system.
- the flue gas 26 may comprise carbon dioxide, steam, SO X , and nitrogen (N 2 ), but it is typically very rich in N 2 .
- the regenerator is operating at a regeneration temperature of from about 500 to about 1000° C., and preferably of from about 650 to about 1000° C.
- the regenerator 14 reactivates the two-component catalyst system so that, when returned to the reactor 12 , the catalyst system is in optimum condition to perform its partial oxidation of methane function.
- the regenerator 14 serves to oxidize the two-component catalyst system, gasify the coke deposited on the catalyst system, and at the same time, to preferably impart sensible heat to the regenerated two-component catalyst system.
- the energy carried by the hot regenerated catalyst system may be used to satisfy at least a portion of the thermal requirements for the reactor 12 .
- the two-component catalyst system is bound to a high heat capacity carrier, preferably alumina, which facilitates the transfer of heat from the regeneration process to the reactor 12 .
- the hot regenerated catalyst is fed back to the reactor 12 via the reactivated catalyst return line 20 and is mixed with the feed gas stream 30 and the mixture is carried upwards through a riser 16 of the reactor 12 with a minimum of back mixing.
- the partial oxidation of methane has been completed and the two-component catalyst system is spent and quickly separated from the syngas where it is returned back to the regenerator 14 via line 23 .
- FIGS. 3 and 4 a schematic depiction of an alternative exemplary reactor and a regenerator system 50 in accordance with an embodiment of the present invention is provided.
- the system comprises a first vessel 52 and a second vessel 54 that are fixed catalyst beds configured as a swing bed reactor arrangement.
- the first and second vessels 52 and 54 are in selective fluid communication with both the feed gas stream 30 and the oxygen containing gas stream 22 via a plurality of valves 56 , 58 , 60 , 62 , 64 , 66 , 68 , and 70 .
- the feed gas stream 30 is advanced to the first vessel 52 through the opened valve 56 .
- Fluid communication of the feed gas stream 30 to the second vessel 54 is prevented by the closed valves 58 and 62 .
- the oxygen containing gas stream 22 is advanced to the second vessel 54 through the opened valve 60 , and is prevented from being fluidly communicated to the first vessel 52 by the closed valves 58 and 62 .
- the first vessel 52 contains the two-component catalyst system (as discussed in the foregoing paragraphs) and the second vessel 54 contains the spent two-component catalyst system (as discussed in the foregoing paragraphs).
- the first vessel 52 effectively operates as a reactor for producing syngas 13 from methane
- a second vessel 54 effectively operates as a regenerator for regenerating the spent two-component catalyst system thereby producing a flue gas stream 26 .
- the first vessel 52 fluidly communicates the syngas 13 through the opened valve 68 where the closed valves 64 and 70 prevent intermixing with the flue gas stream 26 .
- the second vessel 54 fluidly communicates the flue gas stream 26 through the opened valve 66 .
- the valve arrangement switches from opened to closed and vice versa as illustrated in FIG. 4 so as to fluidly communicate the feed gas stream 30 to the second vessel 54 , and to fluidly communicate the oxygen containing gas stream 22 to the first vessel 52 .
- the opened valve 62 and the closed valves 56 and 60 direct the feed gas stream 30 to the second vessel 54 while preventing fluid communication of the feed gas stream 30 to the first vessel 52 .
- the opened valve 58 and the closed valves 56 and 60 direct the oxygen containing gas stream 22 to the first vessel 52 while preventing fluid communication of the oxygen containing gas stream to the second vessel 54 .
- the second vessel 54 effectively operates as a reactor for producing syngas 13 from methane and the first vessel 52 effectively operates as a regenerator to regenerate the spent two-component catalyst system thereby producing flue gas stream 26 .
- the second vessel 54 fluidly communicates the syngas 13 through the opened valve 64 where the closed valves 66 and 68 prevent intermixing with the flue gas stream 26 .
- the first vessel 52 fluidly communicates the flue gas stream 26 through the opened valve 70 .
- the synchronized alternating of the valves 56 , 58 , 60 , 62 , 64 , 66 , 68 , and 70 from opened to closed and vice versa based on the oxidative condition of the two-component catalyst system in each of the vessels 52 and 54 is preferably repeated on a continuous basis to provide a continuous flow system for the production of syngas.
- the first and second vessels 52 and 54 operate at essentially the same operating conditions with regard temperature and pressure for both the partial oxidation of methane and the regeneration of the spent catalyst system to facilitate the continuous production of the syngas 13 .
- Other suitable swing bed reactor arrangements known to those skilled in the art may also be used for partial oxidation of methane and regeneration of the spent catalyst system in accordance with various embodiments of the present invention.
- FIG. 5 is a graphical representation of a material screening evaluation of various catalyst systems in terms of their carbon monoxide selectivity and methane conversion at 860° C.
- the vertical axis (Y) represents the maximum carbon monoxide (CO) selectivity in terms of mole percentage (%), and the horizontal axis (X) represents the methane conversion at maximum CO yield %.
- catalyst systems with a relatively high methane conversion indicate a relatively high conversion level for methane to various products.
- Catalyst systems with a relatively high maximum CO selectivity indicate that the products formed from the methane conversion favor carbon monoxide, and not carbon dioxide or water. Accordingly, catalyst systems with performance results in the upper right-hand corner of the material screening chart are most suitable for producing a high quality syngas stream in accordance with the present invention.
- the catalyst systems evaluated were two-component catalyst systems comprising a metal component and a perovskite component, two-component catalyst systems comprising a metal component and a metal oxide component, and a two-component catalyst system comprising a hydroxyapatite component and a perovskite component.
- the two-component catalyst system with a hydroxyapatite component and a perovskite component, Na 0.15 Ni 0.17 Sr 1.55 PO 4.295 +La 0.8 Sr 0.2 FeO 3 is in the upper most right-hand corner of the chart having a maximum CO selectivity of about 80% and a methane conversion at maximum CO yield % of greater than about 70%.
- catalyst system having a methane conversion at maximum CO yield of about 70% or greater, and a maximum CO selectivity of about 70% or greater are suitable catalyst for partial oxidation of methane in the absence of an oxygen containing atmosphere to provide a high quality syngas reaction product. Accordingly, the Na 0.15 Ni 0.17 Sr 1.55 PO 4.295 +La 0.8 Sr 0.2 FeO 3 two-component catalyst system was found to be the most suitable catalyst system in those evaluated in this material screening study.
- the various embodiments comprise contacting the gas stream with a two-component catalyst system comprising an apatite component and a perovskite component at reaction conditions that convert the methane to syngas.
- the oxygen for the reaction is supplied by the perovskite component rather than in a gaseous stream by an air separator or other costly source.
- the apatite component facilitates partial oxidation of methane by activating the methane so that it readily reacts with the oxygen from the perovskite component at rates that favor a relatively high carbon monoxide selectivity over the production of carbon dioxide or water.
- the syngas produced is preferably high-quality having a relatively high carbon monoxide and hydrogen content with minimal carbon dioxide and water content.
- the apatite component in combination with the perovskite component, very little coke is deposited onto the two-component catalyst during partial oxidation of the methane. Accordingly, when the two-component catalyst system is spent, it can be readily regenerated as needed to maintain catalyst activity and stability over time.
- regenerating the two-component catalyst produces heat that may be supplied to the reactor to at least partially satisfy the energy requirements, such as, for example, in a FCC arrangement, which thereby places less demand on the system compared to conventional processes in terms of thermal resistance to damage and operational cost.
Abstract
Embodiments of a process for producing syngas comprising hydrogen and carbon monoxide from a gas stream comprising methane are provided. The process comprises the step of contacting the gas stream with a two-component catalyst system comprising an apatite component and a perovskite component at reaction conditions effective to convert the methane to the syngas.
Description
- The present invention relates generally to processes and systems for producing synthesis gas, and more particularly relates to processes and systems for producing synthesis gas comprising hydrogen and carbon monoxide from a gas stream comprising methane.
- The combustion stoichiometry of methane gas at 1000° F. is highly exothermic and produces carbon dioxide and water according to the following reaction:
-
CH4+2O2→CO2+2H2O (−190.3 kcal/g mol CH4). - The formed gases are not useful for the production of valuable chemical compounds, and the stability of these products complicates their conversion to more desirable products. Also, further processing is problematic due to the high temperatures generated in the combustion reaction, presenting problems with respect to downstream reactors and catalysts.
- In contrast, useful gases, known as synthesis gas or “syngas”, are produced in the conversion of methane to a gas mixture containing hydrogen and carbon monoxide, for example, according to one of the following reactions:
-
2CH4+2O2→2CO+2H2+2H2O (−64 kcal/g mol CH4) -
2CH4+1.5O2→2CO+3H2+H2O (−34.9 kcal/g mol CH4), or -
2CH4+O2→2CO+H2 (−5.7 kcal/g mol CH4). - The last reaction is the most desirable in terms of both quality of the syngas produced and the minimization of the heat liberated to protect the apparatus and catalyst bed from thermal damage.
- Conventional syngas-generating processes include steam methane reforming and methane partial oxidation (also referred to as catalytic partial oxidation). The choice of a particular route depends primarily on the desired product composition, as determined by its end use. The syngas is typically used to produce methanol, ammonia, or heavier hydrocarbon fuels through Fisher-Tropsch technology for example.
- In the steam methane reforming process, the methane-containing and oxygen-containing feeds are mixed and reacted in a diffusion flame. The oxidized effluent is then passed into a steam reforming reactor zone where the effluent is contacted with a conventional steam reforming catalyst. The catalyst may be present as a simple fixed bed or impregnated into a monolith carrier or ceramic foam. The high temperatures and pressures in the catalytic steam reforming reactor zone place great demands on the reactor, in terms of thermal resistance to damage and operational cost, and on the reforming catalyst, in terms of the catalyst's ability to substantially retain its catalytic activity and stability over many years of use due to substantial coking of the catalyst. Moreover, some of the methane may be burned to provide heat for the energy intensive process and therefore, complete conversion of the methane to the desired end product is not achieved thereby reducing the overall selectivity of the process.
- In the methane partial oxidation process, methane is passed along a nickel-based catalyst for example, and burned at a high temperature in an oxygen lean environment where the methane is partially oxidized to carbon monoxide along with the production of hydrogen and some steam. The methane partial oxidation process uses a higher concentration of oxygen than is found in air and, therefore, requires the use of a costly air separation unit to supply the higher concentration of oxygen. Moreover, as in the steam reforming process, the methane partial oxidation process typically burns a portion of the methane to provide heat for the energy intensive process and therefore, complete conversion of the methane to the desired end product is not achieved thereby reducing the overall selectivity of the process. Furthermore, the methane partial oxidation process results in a substantial amount of coke being deposited onto the catalyst and therefore, catalyst activity and stability over time is substantially reduced.
- Accordingly, it is desirable to provide processes and systems that provide relatively high conversion of methane to syngas, preferably without depositing substantial amounts of coke onto the catalyst so that the catalyst better maintains its activity and stability over time, and which are robust and cost-effective. Furthermore, other desirable features and characteristics of the present invention will become apparent from the subsequent detailed description of the invention in the appended claims, taken in conjunction with the accompanying drawings and this background of the invention.
- Processes and systems for producing syngas from a methane containing gas stream are provided herein. In accordance with an exemplary embodiment, a process for producing syngas comprising hydrogen and carbon monoxide from a gas stream comprising methane is provided. The process comprises the step of contacting the gas stream with a two-component catalyst system comprising an apatite component and a perovskite component at reaction conditions effective to convert the methane to the syngas.
- In accordance with another exemplary embodiment, a system for producing syngas comprising hydrogen and carbon monoxide from a feed gas stream comprising methane is provided. The system comprises a reactor containing a two-component catalyst system comprising an apatite component and a perovskite component. The reactor is configured to receive the feed gas stream and to operate at reactor conditions effective to convert the methane to the syngas thereby converting the two-component catalyst system to a spent two-component catalyst system.
- Embodiments of the present invention will hereinafter be described in conjunction with the following drawing figures, wherein like numerals denote like elements, and wherein:
-
FIG. 1 schematically illustrates a system for producing syngas from a feed gas stream comprising methane in accordance with an exemplary embodiment; -
FIG. 2 is a flowchart of a process for producing syngas from a gas stream comprising methane in accordance with an exemplary embodiment; -
FIG. 3 schematically illustrates a system in a first configuration for producing syngas from a feed gas stream comprising methane in accordance with another exemplary embodiment; -
FIG. 4 schematically illustrates the system depicted inFIG. 3 in a second configuration; and -
FIG. 5 is a graphical representation of carbon monoxide selectivity and methane conversion for various catalyst systems in accordance with an exemplary embodiment of the present invention. - The following Detailed Description is merely exemplary in nature and is not intended to limit the invention or the application and uses of the invention. Furthermore, there is no intention to be bound by any theory presented in the preceding Description of Related Art or the following Detailed Description.
- The various embodiments contemplated herein relate to processes and systems for producing syngas comprising hydrogen and carbon monoxide from a methane containing gas stream. The gas stream is contacted with a two-component catalyst system comprising an apatite component and a perovskite component at reaction conditions that convert the methane to syngas. The oxygen for the reaction is supplied by the perovskite component, which is a metal oxide, rather than by an oxygen containing gas stream that is supplied by an air separator or other costly source. In particular, the inventors have discovered that by using the two-component catalyst system with the apatite component, which in at least one embodiment is a nickel containing oxide, the hydrogen atoms become disassociated from the methane such that the methane is activated and readily reacts with the oxygen supplied from the perovskite component at rates that favor a relatively high carbon monoxide selectivity over the production of carbon dioxide or water. Thus, the syngas produced is of preferably high quality having a relatively high carbon monoxide and hydrogen content with reduced amounts of carbon dioxide and water. Moreover, the inventors have found that by using the apatite component, which is unlike many other nickel catalyst used for the partial oxidation of methane, very little coke is deposited onto the two-component catalyst system. Accordingly, when the two-component catalyst system is spent, it can be readily regenerated as needed to maintain catalyst activity and stability over time. Furthermore, regenerating the two-component catalyst produces heat that may be supplied to the reactor to at least partially satisfy the energy requirements, such as, for example, in a fluidized catalytic cracking arrangement (FCC), which thereby places less demand on the system compared to conventional processes in terms of thermal resistance to damage and operational cost.
- Referring to
FIG. 1 , a schematic depiction of an exemplary reactor and aregenerator system 10 in accordance with an exemplary embodiment of the present invention is provided. Thesystem 10 is configured as a fluidized catalytic cracking (FCC) arrangement. As shown, thesystem 10 comprises areactor 12 that is configured to receive afeed gas stream 30 comprising methane. Thereactor 12 contains a two-component catalyst system comprising an apatite component and a perovskite component. - In an exemplary embodiment, the apatite component has a chemical composition on an anhydrous basis expressed by an empirical formula of:
-
Av(Bt+)wExD(Gu−)yOz, - where A is an alkali metal selected from the group consisting of lithium (Li), sodium (Na), potassium (K), rubidium (Rb), cesium (Cs), and mixtures thereof, v is a mole ratio of A:D (i.e., a ratio of the moles of A to the moles of D) and varies from 0 to about 2, B is a basic metal, w is a mole ratio of B:D and varies from about 1 to about 3, t is the weighted average valence of B and varies from about 2 to about 3, E is a transition metal selected from the group consisting of nickel (Ni), vanadium (V), manganese (Mn), iron (Fe), cobalt (Co), copper (Cu), and mixtures thereof, x is a mole ratio of E:D and varies from 0 to about 0.5, D is a framework component selected from the group consisting of phosphorus (P), V, and mixtures thereof, and G is an anionic species of hydroxide (OH), chlorine (Cl), fluorine (F), carbonate (CO3), and mixtures thereof, u is an average valence of G and varies from about 1 to about 2, y is a mole ratio of G:D and varies from 0 to about 2, z is a mole ratio of O:D and has a value determined by the equation:
-
z=½(y+t·w+2·x+5−u·y), - and when B is calcium (Ca), v is not 0. In a preferred embodiment, G is the anionic species of OH, and the apatite is a hydroxyapatite structured component. In a most preferred embodiment, E is Ni and the apatite component is a nickel-based hydroxyapatite structured component.
- The basic metal B is typically a metal with a rather large cationic radius, generally from about 0.85 Å to about 1.40 Å, and a cationic charge of +2 or +3. These metals are broadly found in the alkaline earth series, rare earth series, and in selected cases in both the transition metal series, such as Cd and Hg, and the main group metals such as lead (Pb). Preferably, B is selected from the group consisting of Ca, strontium (Sr), cadmium (Cd), Pb, barium (Ba), lanthanum (La), europium (Eu), gadolinium (Gd), praseodymium (Pr), neodymium (Nd), samarium (Sm), yttrium (Y), ytterbium (Yb), and mixtures thereof.
- In an exemplary embodiment, the perovskite component comprises perovskite having a chemical composition expressed by an empirical formula of:
-
[Ma1-xMa′x][Mb1-yMb′y]O3-w, - where Ma and Ma', that are identical or different, are chosen from the families of the alkaline earths, the lanthanides or the actinides, more particularly from La, Ce, Pr, Nd, promethium (Pm), Sm, Eu, Gd, terbium (Tb), dysprosium (Dy), holmium (Ho), erbium (Er), thulium (Tm), Yb, lutetium (Lu), Y, magnesium (Mg), Ca, Sr, Ba, and mixtures thereof, Mb and Mb′, that are identical or different, represent one or more atoms chosen from transition metals, and more particularly from Sc, titanium (Ti), V, chromium (Cr), Mn, Fe, Co, Ni, Cu, zinc (Zn), gallium (Ga), and mixtures thereof, x and y, that are identical or different, are greater than or equal to 0 and less than or equal to about 1, and w is such that the perovskite has an electrically neutral structure. In preferred embodiments, the perovskite component comprises La, Sr, Fe, or mixtures thereof.
- In an exemplary embodiment, the two-component catalyst system is configured as particles where each particle comprises the apatite component and the perovskite component. In one example, the apatite component is crystallized onto the perovskite component to form the particles. Alternatively, both the apatite and perovskite components may be bound to a carrier, such as, for example, alumina or silica. In another exemplary embodiment, the two-component catalyst system is a physical mixture of the apatite and perovskite components. Preferably, the two-component catalyst system has a mole ratio of the apatite component to the perovskite component of from about 1:2 to about 2:1, and most preferably of about 1:1.
- Referring also to
FIG. 2 , a process for producing the syngas includes contacting thefeed gas stream 30 with the two-component catalyst system (step 100) in thereactor 12 which is operating at reaction conditions effective to convert the methane to an effluentstream comprising syngas 13 which may be passed along for subsequent processing vialine 15. In one exemplary embodiment, thereactor 12 is operating at a reaction temperature of about 650° C. or greater, and preferably at a reaction temperature of from about 850 to about 1000° C. In another exemplary embodiment, thereactor 12 is operating at a reaction pressure of from about 15 to about 1000 psia, and preferably of from about 15 to about 600 psia, and more preferably of from about 15 to about 350 psia. Preferably, the atmosphere inside thereactor 12 is substantially devoid of gaseous oxygen so that the oxygen source for the partial oxidation of methane comes primarily from the perovskite component. Without being limited by theory, the inventors believe that by limiting the source of oxygen to the perovskite component, the partial oxidation of methane will primarily favor producing carbon monoxide and hydrogen over the more highly oxidized and undesirable products of carbon dioxide and water. - In an exemplary embodiment, the apatite component of the two-component catalyst system activates the methane (step 102) to form activated methane. The activated methane then readily oxidizes with oxygen from the perovskite component (step 104) to form the
syngas 13. During the partial oxidation process of the methane, the perovskite component becomes oxygen depleted, and a relatively small amount of carbonaceous byproduct, termed coke, is deposited on the two-component catalyst system reducing its catalytic activity and forming a spent two-component catalyst system. - A
regenerator 14 is in fluid communication with thereactor 12 to receive the spent two-component catalyst system vialine 23. Theregenerator 14 is configured to receive an oxygen containinggas stream 22, preferably air, from an outside source. The regenerator 14 operating at regeneration conditions receives the oxygen containinggas stream 22, oxidizes the perovskite component and burns the coke off the spent two-component catalyst system to regenerate the spent two-component catalyst system (step 106) thereby producing aflue gas 26 that exits aflue gas line 28 to a flue gas system. Theflue gas 26 may comprise carbon dioxide, steam, SOX, and nitrogen (N2), but it is typically very rich in N2. In one exemplary embodiment, the regenerator is operating at a regeneration temperature of from about 500 to about 1000° C., and preferably of from about 650 to about 1000° C. - The
regenerator 14 reactivates the two-component catalyst system so that, when returned to thereactor 12, the catalyst system is in optimum condition to perform its partial oxidation of methane function. Theregenerator 14 serves to oxidize the two-component catalyst system, gasify the coke deposited on the catalyst system, and at the same time, to preferably impart sensible heat to the regenerated two-component catalyst system. The energy carried by the hot regenerated catalyst system may be used to satisfy at least a portion of the thermal requirements for thereactor 12. In an exemplary embodiment, the two-component catalyst system is bound to a high heat capacity carrier, preferably alumina, which facilitates the transfer of heat from the regeneration process to thereactor 12. - The hot regenerated catalyst is fed back to the
reactor 12 via the reactivatedcatalyst return line 20 and is mixed with thefeed gas stream 30 and the mixture is carried upwards through ariser 16 of thereactor 12 with a minimum of back mixing. At the top 18 of theriser 16, the partial oxidation of methane has been completed and the two-component catalyst system is spent and quickly separated from the syngas where it is returned back to theregenerator 14 vialine 23. - Referring to
FIGS. 3 and 4 a schematic depiction of an alternative exemplary reactor and aregenerator system 50 in accordance with an embodiment of the present invention is provided. The system comprises afirst vessel 52 and asecond vessel 54 that are fixed catalyst beds configured as a swing bed reactor arrangement. The first andsecond vessels feed gas stream 30 and the oxygen containinggas stream 22 via a plurality ofvalves FIG. 3 , thefeed gas stream 30 is advanced to thefirst vessel 52 through the openedvalve 56. Fluid communication of thefeed gas stream 30 to thesecond vessel 54 is prevented by theclosed valves gas stream 22 is advanced to thesecond vessel 54 through the openedvalve 60, and is prevented from being fluidly communicated to thefirst vessel 52 by theclosed valves first vessel 52 contains the two-component catalyst system (as discussed in the foregoing paragraphs) and thesecond vessel 54 contains the spent two-component catalyst system (as discussed in the foregoing paragraphs). Accordingly, thefirst vessel 52 effectively operates as a reactor for producingsyngas 13 from methane, and asecond vessel 54 effectively operates as a regenerator for regenerating the spent two-component catalyst system thereby producing aflue gas stream 26. Thefirst vessel 52 fluidly communicates thesyngas 13 through the openedvalve 68 where theclosed valves flue gas stream 26. Thesecond vessel 54 fluidly communicates theflue gas stream 26 through the openedvalve 66. - When the two-component catalyst system in the
first vessel 52 is spent and the spent two-component catalyst system in thesecond vessel 54 is regenerated, the valve arrangement switches from opened to closed and vice versa as illustrated inFIG. 4 so as to fluidly communicate thefeed gas stream 30 to thesecond vessel 54, and to fluidly communicate the oxygen containinggas stream 22 to thefirst vessel 52. In particular, the openedvalve 62 and theclosed valves feed gas stream 30 to thesecond vessel 54 while preventing fluid communication of thefeed gas stream 30 to thefirst vessel 52. The openedvalve 58 and theclosed valves gas stream 22 to thefirst vessel 52 while preventing fluid communication of the oxygen containing gas stream to thesecond vessel 54. In this scenario, thesecond vessel 54 effectively operates as a reactor for producingsyngas 13 from methane and thefirst vessel 52 effectively operates as a regenerator to regenerate the spent two-component catalyst system thereby producingflue gas stream 26. Thesecond vessel 54 fluidly communicates thesyngas 13 through the openedvalve 64 where theclosed valves flue gas stream 26. Thefirst vessel 52 fluidly communicates theflue gas stream 26 through the openedvalve 70. - The synchronized alternating of the
valves vessels second vessels syngas 13. Other suitable swing bed reactor arrangements known to those skilled in the art may also be used for partial oxidation of methane and regeneration of the spent catalyst system in accordance with various embodiments of the present invention. -
FIG. 5 is a graphical representation of a material screening evaluation of various catalyst systems in terms of their carbon monoxide selectivity and methane conversion at 860° C. The vertical axis (Y) represents the maximum carbon monoxide (CO) selectivity in terms of mole percentage (%), and the horizontal axis (X) represents the methane conversion at maximum CO yield %. In general, catalyst systems with a relatively high methane conversion indicate a relatively high conversion level for methane to various products. Catalyst systems with a relatively high maximum CO selectivity indicate that the products formed from the methane conversion favor carbon monoxide, and not carbon dioxide or water. Accordingly, catalyst systems with performance results in the upper right-hand corner of the material screening chart are most suitable for producing a high quality syngas stream in accordance with the present invention. - The catalyst systems evaluated were two-component catalyst systems comprising a metal component and a perovskite component, two-component catalyst systems comprising a metal component and a metal oxide component, and a two-component catalyst system comprising a hydroxyapatite component and a perovskite component. As indicated in
FIG. 4 , the two-component catalyst system with a hydroxyapatite component and a perovskite component, Na0.15Ni0.17Sr1.55PO4.295+La0.8Sr0.2FeO3, is in the upper most right-hand corner of the chart having a maximum CO selectivity of about 80% and a methane conversion at maximum CO yield % of greater than about 70%. The inventors have found that catalyst system having a methane conversion at maximum CO yield of about 70% or greater, and a maximum CO selectivity of about 70% or greater are suitable catalyst for partial oxidation of methane in the absence of an oxygen containing atmosphere to provide a high quality syngas reaction product. Accordingly, the Na0.15Ni0.17Sr1.55PO4.295+La0.8Sr0.2FeO3 two-component catalyst system was found to be the most suitable catalyst system in those evaluated in this material screening study. - Accordingly, processes and systems for producing syngas comprising hydrogen and carbon monoxide from a methane containing gas stream have been described. The various embodiments comprise contacting the gas stream with a two-component catalyst system comprising an apatite component and a perovskite component at reaction conditions that convert the methane to syngas. The oxygen for the reaction is supplied by the perovskite component rather than in a gaseous stream by an air separator or other costly source. Moreover, the apatite component facilitates partial oxidation of methane by activating the methane so that it readily reacts with the oxygen from the perovskite component at rates that favor a relatively high carbon monoxide selectivity over the production of carbon dioxide or water. Thus, the syngas produced is preferably high-quality having a relatively high carbon monoxide and hydrogen content with minimal carbon dioxide and water content. Moreover, by using the apatite component in combination with the perovskite component, very little coke is deposited onto the two-component catalyst during partial oxidation of the methane. Accordingly, when the two-component catalyst system is spent, it can be readily regenerated as needed to maintain catalyst activity and stability over time. Furthermore, regenerating the two-component catalyst produces heat that may be supplied to the reactor to at least partially satisfy the energy requirements, such as, for example, in a FCC arrangement, which thereby places less demand on the system compared to conventional processes in terms of thermal resistance to damage and operational cost.
- While at least one exemplary embodiment has been presented in the foregoing Detailed Description, it should be appreciated that a vast number of variations exist. It should also be appreciated that the exemplary embodiment or exemplary embodiments are only examples, and are not intended to limit the scope, applicability, or configuration of the invention in any way. Rather, the foregoing Detailed Description will provide those skilled in the art with a convenient road map for implementing an exemplary embodiment of the invention, it being understood that various changes may be made in the function and arrangement of elements described in an exemplary embodiment without departing from the scope of the invention as set forth in the appended Claims and their legal equivalents.
Claims (20)
1. A process for producing syngas comprising hydrogen and carbon monoxide from a gas stream comprising methane, the process comprising the step of:
contacting the gas stream with a two-component catalyst system comprising an apatite component and a perovskite component at reaction conditions effective to convert the methane to the syngas.
2. The process according to claim 1 , wherein the reaction conditions include a reaction temperature of about 650° C. or greater.
3. The process according to claim 2 , wherein the reaction temperature is from about 850 to about 1000° C.
4. The process according to claim 1 , wherein the reaction conditions include a reaction pressure of about 15 to about 1000 psia.
5. The process according to claim 1 , wherein the two-component catalyst system is a physical mixture of apatite catalyst particles and perovskite catalyst particles.
6. The process according to claim 1 , wherein the two-component catalyst system comprises particles each comprising the apatite component and the perovskite component.
7. The process according to claim 6 , wherein each of the particles further comprises alumina or silica bound to the apatite and perovskite components.
8. The process according to claim 1 , wherein the apatite component has a chemical composition on an anhydrous basis expressed by an empirical formula of:
Av(Bt+)wExD(Gu−)yOz
Av(Bt+)wExD(Gu−)yOz
where A is an alkali metal selected from the group consisting of Li, Na, K, Rb, Cs, and mixtures thereof, v is a mole ratio of A:D and varies from 0 to about 2, B is a basic metal selected from the group consisting of Ca, Sr, Cd, Pb, Ba, La, Eu, Gd, Pr, Nd, Sm, Y, Yb, and mixtures thereof, w is a mole ratio of B:D and varies from about 1 to about 3, t is the weighted average valence of B and varies from about 2 to about 3, E is a transition metal selected from the group consisting of Ni, V, Mn, Fe, Co, Cu, and mixtures thereof, x is a mole ratio of E:D and varies from 0 to about 0.5, D is a framework component selected from the group consisting of P, V, and mixtures thereof, and G is an anionic species of OH, Cl, F, CO3, and mixtures thereof, u is an average valence of G and varies from about 1 to about 2, y is a mole ratio of G:D and varies from 0 to about 2, z is a mole ratio of 0 to D and has a value determined by the equation:
z=½(v+t·w+2·x+5−u·y),
z=½(v+t·w+2·x+5−u·y),
and when B is Ca, v is not 0.
9. The process according to claim 8 , wherein G is the anionic species of OH, and the apatite is a hydroxyapatite, defining the apatite component as a hydroxyapatite component.
10. The process according to claim 1 , wherein the perovskite component comprises perovskite having a chemical composition expressed by an empirical formula of:
[Ma1-xMa′x][Mb1-yMb′y]O3-w
[Ma1-xMa′x][Mb1-yMb′y]O3-w
where Ma and Ma′ are selected from the group consisting of La, Ce, Pr, Nd, Pm, Sm, Eu, Gd, Tb, Dy, Ho, Er, Tm, Yb, Lu, Y, Mg, Ca, Sr, Ba, and mixtures thereof, Mb and Mb′ are transition metals, x and y are greater than or equal to 0 and less than or equal to about 1, and w is such that the perovskite has an electrically neutral structure.
11. The process according to claim 10 , wherein Mb and Mb′ are selected from the group consisting of Sc, Ti, V, Cr, Mn, Fe, Co, Ni, Cu, Zn, Ga, and mixtures thereof.
12. The process according to claim 1 , wherein the two-component catalyst system has a methane conversion at maximum CO yield of about 70% or greater, and a maximum CO selectivity of about 70% or greater.
13. The process according to claim 1 , wherein the two-component catalyst system has a mole ratio of the apatite component to the perovskite component of about 1:2 to about 2:1.
14. The process according to claim 1 , wherein the step of contacting the gas stream with the two-component catalyst system comprises activating the methane with the apatite component to form an activated methane, and oxidizing the activated methane with the perovskite component to form the syngas and produce a spent two-component catalyst system, wherein the process further comprises the step of contacting the spent two-component catalyst system with gas comprising oxygen at regeneration conditions effective to regenerate the spent two-component catalyst system, producing a regenerated two-component catalyst system.
15. A system for producing syngas comprising hydrogen and carbon monoxide from a feed gas stream comprising methane, the system comprising a reactor containing a two-component catalyst system comprising an apatite component and a perovskite component, the reactor configured to receive the feed gas stream and to operate at reactor conditions effective to convert the methane to the syngas thereby converting the two-component catalyst system to a spent two-component catalyst system.
16. The system according to claim 15 , further comprising a regenerator containing the spent two-component catalyst system and configured to receive an oxygen containing gas stream and to operate at regeneration conditions effective to regenerate the spent two-component catalyst system to form a regenerated two-component catalyst system.
17. The system according to claim 16 , wherein the reactor and the regenerator are configured as a fluidized catalytic cracking (FCC) arrangement such that the regenerator is in fluid communication with the reactor to receive the spent two-component catalyst system from the reactor and to advance the regenerated two-component catalyst system to the reactor.
18. The system according to claim 17 , wherein the two-component catalyst system comprises particles each comprising the apatite component and the perovskite component.
19. The system according to claim 18 , wherein each of the particles further comprises one of alumina and silica bound to the apatite and perovskite components.
20. The system according to claim 16 , wherein the reactor and the regenerator are configured as a swing bed reactor arrangement that comprises a first vessel and a second vessel, the first and second vessels cooperatively configured to alternate between each other to define the reactor and the regenerator based on the oxidative condition of the two-component catalyst system.
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Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN103816913A (en) * | 2014-03-06 | 2014-05-28 | 太原理工大学 | Catalyst for preparing synthetic gas by reforming of methane and carbon dioxide as well as preparation method and application of catalyst |
CN105854885A (en) * | 2016-04-07 | 2016-08-17 | 太原理工大学 | Catalyst for reforming methane and carbon dioxide to prepare synthetic gas as well as preparation method and application thereof |
WO2016130393A1 (en) * | 2015-02-13 | 2016-08-18 | Sabic Global Technologies B.V. | Methods for conversion of methane to syngas |
Families Citing this family (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EA027816B1 (en) | 2010-05-24 | 2017-09-29 | Силурия Текнолоджиз, Инк. | Nanowire catalysts |
EA029867B1 (en) | 2011-05-24 | 2018-05-31 | Силурия Текнолоджиз, Инк. | Catalysts for petrochemical catalysis |
US8962517B2 (en) | 2011-11-29 | 2015-02-24 | Siluria Technologies, Inc. | Nanowire catalysts and methods for their use and preparation |
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EP3194070B1 (en) | 2014-09-17 | 2020-12-23 | Lummus Technology LLC | Catalysts for oxidative coupling of methane and oxidative dehydrogenation of ethane |
US9662639B2 (en) * | 2015-05-11 | 2017-05-30 | University Of Wyoming | Catalytic effects of oxygen carrier based chemical-looping reforming of CH4 with CO2 |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6544439B1 (en) * | 2000-12-22 | 2003-04-08 | Uop Llc | Low coke formation catalysts and process for reforming and synthesis gas production |
US7070752B2 (en) * | 2001-05-01 | 2006-07-04 | The Boc Group, Inc. | Supported perovskite-type oxides and methods for preparation thereof |
US20070172418A1 (en) * | 2006-01-25 | 2007-07-26 | Slager Terry L | Regeneration of complex metal oxides for the production of hydrogen |
US20110201854A1 (en) * | 2010-02-17 | 2011-08-18 | Kocal Joseph A | Low oxygen biomass-derived pyrolysis oils and methods for producing the same |
Family Cites Families (12)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4418008A (en) * | 1982-02-24 | 1983-11-29 | Exxon Research And Engineering Co. | Process for increasing the activity of perovskite catalysts and hydrocarbon treating processes using the activated catalyst |
US5149516A (en) | 1990-10-15 | 1992-09-22 | Mobil Oil Corp. | Partial oxidation of methane over perovskite catalyst |
FR2696109B1 (en) | 1992-09-28 | 1994-11-04 | Inst Francais Du Petrole | Oxidation catalyst and partial methane oxidation process. |
US6143203A (en) | 1999-04-13 | 2000-11-07 | The Boc Group, Inc. | Hydrocarbon partial oxidation process |
EP1263678A1 (en) * | 2000-02-18 | 2002-12-11 | Conoco Inc. | Chromium-rare earth based catalysts and process for converting hydrocarbons to synthesis gas |
FR2817860B1 (en) | 2000-12-07 | 2003-09-12 | Air Liquide | PROCESS FOR THE PREPARATION OF A LOW THICKNESS CERAMIC MATERIAL WITH CONTROLLED SURFACE POROSITY GRADIENT, CERAMIC MATERIAL OBTAINED, ELECTROCHEMICAL CELL AND CERAMIC MEMBRANE COMPRISING THE SAME |
FR2826956B1 (en) | 2001-07-04 | 2004-05-28 | Air Liquide | PROCESS FOR PREPARING A LOW THICKNESS CERAMIC COMPOSITION WITH TWO MATERIALS, COMPOSITION OBTAINED, ELECTROCHEMICAL CELL AND MEMBRANE COMPRISING IT |
ITMI20011519A1 (en) * | 2001-07-17 | 2003-01-17 | Uni Degli Studi Di L Aquila | SOLID SOLUTIONS WITH PEROVSKITIC STRUCTURE INCLUDING NOBLE METALS USEFUL AS CATALYSTS |
EP1419814A1 (en) | 2002-11-15 | 2004-05-19 | L'AIR LIQUIDE, Société Anonyme à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des | Perovskite catalyst for the partial oxidation of natural gas |
FR2879478B1 (en) | 2004-12-17 | 2007-10-26 | Inst Francais Du Petrole | COBALT CATALYST FOR THE FISHER-TROPSCH SYNTHESIS |
EP1795260A1 (en) | 2005-12-07 | 2007-06-13 | L'AIR LIQUIDE, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude | Catalyst comprising a solid support, an oxide and an active metal phase grafted on the oxide; process for its preparation and use |
US20090123354A1 (en) | 2007-11-14 | 2009-05-14 | Deng-Yang Jan | Selective Oxidation Agent of Hydrocarbons to Synthesis Gas Based on Separate Particles of O-Carrier and Hydrocarbon Activator |
-
2010
- 2010-11-02 US US12/917,781 patent/US8414798B2/en not_active Expired - Fee Related
-
2011
- 2011-10-28 WO PCT/US2011/058231 patent/WO2012061216A2/en active Application Filing
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6544439B1 (en) * | 2000-12-22 | 2003-04-08 | Uop Llc | Low coke formation catalysts and process for reforming and synthesis gas production |
US7070752B2 (en) * | 2001-05-01 | 2006-07-04 | The Boc Group, Inc. | Supported perovskite-type oxides and methods for preparation thereof |
US20070172418A1 (en) * | 2006-01-25 | 2007-07-26 | Slager Terry L | Regeneration of complex metal oxides for the production of hydrogen |
US20110201854A1 (en) * | 2010-02-17 | 2011-08-18 | Kocal Joseph A | Low oxygen biomass-derived pyrolysis oils and methods for producing the same |
Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN103816913A (en) * | 2014-03-06 | 2014-05-28 | 太原理工大学 | Catalyst for preparing synthetic gas by reforming of methane and carbon dioxide as well as preparation method and application of catalyst |
CN103816913B (en) * | 2014-03-06 | 2016-03-30 | 太原理工大学 | A kind of Catalysts and its preparation method of synthesizing gas by reforming methane with co 2 and application |
WO2016130393A1 (en) * | 2015-02-13 | 2016-08-18 | Sabic Global Technologies B.V. | Methods for conversion of methane to syngas |
CN105854885A (en) * | 2016-04-07 | 2016-08-17 | 太原理工大学 | Catalyst for reforming methane and carbon dioxide to prepare synthetic gas as well as preparation method and application thereof |
CN105854885B (en) * | 2016-04-07 | 2018-10-30 | 太原理工大学 | A kind of catalyst of synthesizing gas by reforming methane with co 2 and its preparation method and application |
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